Process for preparing linear olefins



United States Patent US. Cl. 260-68315 Claims ABSTRACT THE DISCLOSURE Ethylene is polymerized to form low molecular weight linear alpha olefins by reaction above 50 p.s.i.a., below 25 C. and in the presence of a catalyst which is the reaction product of an aluminum alkyl and a transition metal halide, the reaction being effected in a polar solvent, the the product being useful as a chemical intermediate.

This application is a continuation-impart of Ser. No. 428,836, filed Jan. 28, 1965 and now abandoned, which in turn is a continuation-in-part of Ser. No. 55,845, filed Sept. 8, 1960, which is now U.S. Patent No. 3,168,588.

This invention relates to a novel method of preparing linear olefins. In particular, this invention relates to a novel process for polymerizing ethylene to obtain a distribution of linear alpha olefin products having a number average molecular weight of from about 70 to about 300. More particularly, this invention relates to a novel process for polymerizing ethylene to obtain a product comprising at least 90 mole percent even numbered linear olefins having molecular weights in the range of from 56 to 2000. Most preferably, this invention relates to a process for polymerizing ethylene to produce a product comprising essentially linear olefins in the C to C range.

It has been shown in the prior art (US. Patent No. 2,993,942) that hydrocarbon lubricating oils having a molecular weight in the range of 80 to 2000 could be prepared by polymerizing ethylene with controlled catalyst, diluents and under controlled temperature-s. The catalyst consisted of a transition metal halide and a halogenated aluminum alkyl compound. It has also been found that increased oil yields, catalyst reactivity and improved molecular weight control could be obtained by the addition of a minor amount of a lower alkanol, as a catalyst modifier to the reaction system. Both the modified and unmodified systems described above resulted, under the conditions in the reaction in the production of major portions of other than linear alpha olefin products, particularly Type II '(RHC=CHR),

and

Type IV olefins, the relative amount of each type being dependent upon the selection of solvent for the reaction.

It has now been discovered that ethylene can be polymerized under controlled conditions to produce a reaction product containing at least 9 mole percent linear olefin products having a number average molecular weight of up to about 300. The process of this invention requires the control of certain critical reaction variables comprising the mole ratio of ethylene to product, the use of a particular soluble catalyst, and temperature and pressure ranges.

The catalyst employed in this invention is a critical feature in obtaining the desired low molecular weight linear olefin polymers. The catalyst of this invention is a complex reaction product which is substantially soluble in the polymerization system and is obtained by mixing a reducible heavy transition metal halide selected from Group IV-B to VI-B or VIII metal with an aluminum alkyl compound such that the ultimate formula of the aluminum alkyl compound is AlR,,X wherein n is equal to or greater than 1 but less than 2, R is alkyl, cycloalkyl or aralkyl, preferably containing 1 to 20 carbon atoms, for example, methyl ethyl, hexyl, decyl, dodecyl, isobutyl, cyclohexyl, benzyl, etc., and X is Cl, Br or I. While most transition metal halides are suitable components of the catalyst complex when the desired product is the branched chain olefins of the prior art, it has been found that compounds such as VCL, and FeCl;, are unsuitable for the preparation of linear alpha olefins. The preferred transition metal catalyst component is a titanium compound having a valency of 3 or 4, preferably 4, and may be represented by the formula: TiX A wherein a=3 or 4, b=0 or 1 and a-|-b=3 or 4, X=Cl or Br and A is Cl or Br or an anion derived from a protonic compound such as an alcohol (ROH) or a carboxylic acid (RCOOH). The R of the protonic compound may be an alkyl, aryl, aralkyl or cycloalkyl group. The TiX A component may be made in situ by reacting TiX, with the protonic compound. Thus, the preferred transition metal component of this invention may be selected from the group TiX TiX OR and TiX OOCR'. Typical examples of such compounds are TiCl TiBr TiX OC H and TiX OOCCH As set forth above, it is essential that the aluminum alkyl catalyst after reaction with the transition metal halide have the formula AlR X The aluminum alkyl compound is employed in a molar ratio to the transition metal halide of 0.5/1 to 100/1, preferably 1/1 to 20/ 1, more preferably 1/1 to 12/1. In an embodiment using a dialkyl aluminum halide, e.g., diethyl aluminum chloride, the aluminum compounds is preferably employed in a molar ratio to the transition metal compound of 1/1. In less preferred embodiments, hydrocarbon aluminum derivatives such as aluminum triethyl and aluminum triisobutyl may be employed as the starting aluminum compounds. These latter materials, however, require higher ratios of transition metal halide to aluminum compound and due to the varied nature of the catalyst complex may in some instances result either in low activity, formation of higher molecular weight solid polymers or excessive branching and isomerization of the olefin products. Mixtures of the alkyl aluminum compounds may be used advantageously to control catalyst activity and product distribution. Catalyst concentration is normally in the range of 0.1 to 10 grams per liter of diluent.

Ethylene is unique in the instant invention in that other olefins do not respond to give linear alpha olefins. Therefore, it is desirable to use essentially pure ethylene or mixtures of ethylene with inert gases as the feed for the process of this invention. Ethylene feeds containing minor amounts of other olefins may be used provided that the extent of copolymerization does not decrease product linearity below Alcohols may be used to modify the catalysts to control product molecular weight, permit operation at higher temperatures and/or lower pressures with improved selectivity, etc. However, alcohols are not essential for this process if the catalyst composition and polymerization conditions are controlled with-in a critical range.

The lower alkanols which may be utilized are those in the C to C range, preferably C to C The improvement from the use of the alkanol increases with molecular weight within the stated range. It has also been found that the structure of the alkanol is important. For the butanol series the yield increased markedly upon changing from primary to secondary to tertiary alcohol. Also, the selectivity to polymer oil (lower average molecular weight) was considerably higher for secondary butanol and tertiary butanol than for isobutanol. Thus, the alkanols that can be used include methanol, ethanol, n-propanol, isopropanol, n-butanol, sec-butanol, tertiary butanol, isobutanol and all of the C and C alcohols. C to C diols in which the hydroxy groups are not attached to adjacent carbon atoms are also useful. Especially preferred and desirable are: tertiary butanol, secondary butanol, isoor n-butanol, and isopropanol. These alkanols are utilized in a minor amount, i.e., so that the ratio of ROH/ R (based on aluminum alkyl) after reduction reduction of the transition metal is not greater than 0.5 (preferably 0.2 to 0.33). The alkanol can be added either to the transition metal halide or the aluminum alkyl halide prior to the addition of the other component. It is preferred to add it, however, to the aluminum alkyl halide.

Although Lewis bases, such as ethers or tertiary amines, are known to be effective additives for making solid polymers at higher rates with Ziegler-type catalysts, their use with the present catalysts leads to drastic loss of activity and selectivity to liquid linear olefins. Thus, the mode of action of this catalyst under the conditions of this invention appears to be quite different from the conventional catalysts.

Polymerization diluent is a critical feature of this invention. The useable diluents are polar aromatic hydrocarbon and halohydrocarbon solvents. Aliphatic and naphthenic diluents are completely unsatisfactory when used alone since they produce only high molecular weight, solid polyethylene. The preferred diluents are aromatic and halogenated aromatic solvents since they result in the production of linear alpha olefins in the desired molecular weight range while employing the most efficient temperatures and ethylene pressures. Less preferred solvents are halogenated aliphatic compounds which, while capable of being employed in the process of preparing linear alpha olefins, require the utilization of higher pressures to achieve average molecular weights of the same order as the preferred solvents. The preferred diluents include halogenated aromatics such as chlorobenzene, dichlorobenzene, chlorotoluene, etc., and aromatics such as benzene, toluene, xylene, tetrahydronaphthalene, etc. The suitable halogenated aliphatic diluents include methyl chloride, ethyl chloride, dichloromethane, etc. Mixtures of these diluents may be used. Also, mixtures of the above types with aliphatic or naphthenic solvents may be used provided the polar types comprise a minimum of about 40% of the total. The diluent or diluent mixture may be used to control the product molecular weight distribution to obtain maximum selectivity to the desired olefin products.

The critical variable with respect to the selective synthesis of linear alpha olefins is the ethylene pressure. The prior art obtained highly branched olefins (60%) when using the closely related catalyst and diluent systems at pressures of 7 to 30 p.s.i.g. It has now been found that ethylene pressures above 50 p.s.i.a. are essential for making linear olefins in high selectivities. Although some variations are permitted depending upon the catalyst composition, diluent and temperature, the perferred pressures are above about 80 to 100 p.s.i.a. in order to produce commercially attractive yields (at least above 5 weight percent and preferably above 10 weight percent olefins in the reactor efiluent, efiluent being diluent and reaction product) of linear alpha olefins having a purity greater than about The most preferred range is above and further, above 500 p.s.i.a. ethylene pressure. At very high ethylene pressures the process may become uneconomical because of the equipment requirements and ethylene recycle.

The most critical variable found with respect to the selective snythesis of linear olefins is the ethylene concentration. It has been found that the ratio of moles of ethylene to the moles of products must be above 0.8 throughout the reaction in order to effect the selective synthesis of ethylene to linear olefins. The preferred ratio of ethylene to products is above about 2. The upper limit of the mole ratio of ethylene to product is not critical. The mole ratio of ethylene to product must be above 0.8 or the product formed contains more than 10% branched chain olefins at product concentrations required to produce commercially attractive yields.

The maximum temperature employable in the process for obtaining linear alpha olefins is about +25 C. Preferably temperatures in the range of 30 C. to +10 C. are employed. The selection of a particular temperature within the above-specified range for achieving the highest selectivity to linear alpha olefins is dependent upon the choice of solvent, catalyst and ethylene pressure.

Reaction times are not particularly critical when operating under the preferred conditions, and they will normally be in the range of 0.1 to 5 hours to obtain product concentrations above 5 weight percent in the diluent. The process may be carried out in batch or continuous operation. However, high product purity and high concentration are achieved most easily in batch reactions or in continuous systems operating under substantially plug flow conditions. A reactor may consist of a long pipe through which the diluent and catalyst flow with ethylene being introduced at many points along the pipe to maintain the desired ethylene concentration. In such a system, monomer concentration need not be constant but may be controlled differently in different sections of the reactor to achieve the best balance of activity, molecular weight and product purity.

The invention will be further understood by reference to the following examples.

EXAMPLE 1 A solution of 0.006 mole TiCL, in 400 ml. chlorobenzene was added to a stirred autoclave under dry nitrogen. Ethylene was added at 20 C. and 3 to 5 p.s.i.a. for S to 8 minutes followed by a solution of 0.006 mole AlEt Cl and 0.012 mole AlEtCl in 100 ml. chlorobenzene. The mixture was stirred 30 minutes for the catalyst pretreatment. The temperature was then reduced to --5 C. and the ethylene pressure was increased to 20 p.s.i.a. in Run 1 and 40 p.s.i.a. in Run 2. The high purity ethylene was added continuously to maintain the respective pressures. After 2.5 hours for Run 1 and 1 hour for Run 2, the reactions were terminated :by draining the reactor contents into 20 ml. isopropyl alcohol. The volume increase amounted to 85 ml. in Run 1 and 70 ml. in Run 2.

Upon standing, the reaction solution from Run 1 remained liquid, whereas the initially clear solution from Run 2 crystallized. This showed that the product obtained in Run 2 at the higher pressure contained linear, crystallizable olefins. Upon distillation of the product from Run 2 to remove chlorobenzene, the C. bottoms amounted to 52.8 grams which was predominantly wax. This is in contrast to Run 1 and the atmospheric pressure polymerizations in the art which made lubricating oils or vaseline-like products having low solidifying points because of their branched structures.

EXAMPLE 2 .A series of runs were made to determine the effect of ethylene pressure on product linearity. All were carried out at 20 C. using 500 ml. of either chlorobenzene or xylene diluent. The proportions of catalyst components were maintained constant, although total catalyst concen- 3,441,680 6 tration was varied by a factor of four. The TiCl in 400 except that no alcohol modifier was used and the ml. diluent was added to the reactor under dry nitrogen AlR X was varied from AlEtCl to AlEt Cl to and cooled to 20 C. The t-butyl alcohol and AlEt Cl AlEt Cl. The results summarized in Table II show that were mixed 5 minutes in 100 ml. diluent before adding AlEtCl produces the desired products but activity is low; the AlEtCl The latter was added to the reactor and AlEt Cl is effective and more active; AIEt Cl is least the total mixture allowed to react minutes at C. 5 active for making liquid olefins and yields almost exclu- High purity ethylene was obtained by passing commersively high molecular weight polyethylene. The small cial C.P. ethylene over copper oxide at 205 C. to reamount of liquid olefins made w1th AlEt Cl probably move oxygen and then through 3A molecular sieves to came from the small amount (less than 1 mole per mole remove water. It was stored in a one gallon reservoir at TiCli of AlEtCl which would be obtamed by reduclng 1000 p.s.i.g. After the catalyst pretreatment, the reactor 10 or alkylating the TiCl Since a 12/1 Al/T1 who was was brought to reaction pressure very rapidly while the used, the main product (solid polymer) was obtained reactor contents were subjected to high speed stirring. from the l l AlEt Cl rather than the 1 AlEtCl Ethylene was added as necessary to maintain pressure and However, 1n Run 13 the catalyst consisted of equlmolar the temperature was kept at -20 C. by circulating cool- 15 amounts of AlEt Cl and T1Cl Therefore, after alkylatant h h fl around h t mg or reducing the T1Cl the AlEt Cl would have been The results are summarized in Table 1. After killing the converted to AlEtCl to an appreciable extent. Only liquid catalyst i h about to 50 1 th l containing product was obtained 1n agreement wlththls mechanism.

NaOH, the product was water-washed twice and dried Thus, A1Et2C1 Or even AlEts Could be to alkylate Q Over K2CQ3 Th products ere analyzed quantitatively 20 reduce the T1Cl as long as the reaction product is for olefi types by infrared, and the split between linear AlR X where n is at least 1 but less than 2.

and branched products was determined by quantitative gas The runs m a d in table 11 below were 1 hour 0 chromatography on a sample of total reactor product, runs at 20 C.

TABLE II Mmoles C1114 Liquid Solid Run Al cpd. A lTiCh Dlluent (p.s.i.a.) olefins, g. polymer, g.

AlEtCl 12/1 01121501 150 7 0 10 111110.501 12/1 CaH5Cl- 15s 10 0 1 AlEtgCl 12/1 0511501.. 150 3 148 13 AlEtzCl Xylene 105 13 0 1 Molecular weight=1,670,000. Using a 4-foot column of silicone gum rubber and tem- EXAMPLE 4 perature programming, it was possible to obtain the yield The effect of polarity of the reaction solvent on the of each product up to C H Product linearity is expressd as mole percentin the C12 20 fraction It was com average molecular weight of the alpha olefin product is shown by the following experiments carried out in the pared n the 12 z0 because? i was the most manner described in Examples 2 and 3. Because of the curate analysis 0I1 g volatlhty losses from C410 widely different results obtained with the solvents studied, fraction and p r fesqhltlofl of the branched and it is difiicult to make comparisons under identical condilin ar OlefiIlS above 20- The llneanty of the total Product tions. However, the trend of decreasing molecular weight s muc higher than that Shown for the 1240 fractloh with increasing solvent polarity is clear from the data cause in all pressure runs the C fraction is essentially u i d i T bl HL 100% linear, and it is a major portion of the total prod- TABLE In uct.

As shown in Table I, the selectivity to linear alpha g f 5 5; M11 olefins increases sharply above about p.s.1.a. and be- 6/6/1/1 mHeptane 165 4 435,000 comes greater than above about p.s.1.a. At 6/6/1/1 50% n-Heptane, 65 143 still higher ethylene pressures, selectivity rapidly ap 6/6/1/1 ggg y 124 proaches 100% in the C fraction. Excellent results 6/6/1/1 0511501- 160 113 12/12/2/2 043G501. 500 147 were obtained w1th either chlorobenzene or xylene d1lu- 12/12/2/2 005154012 500 142 ent. in addition to the effect on olefin linearity, ethylene glggig fi:- g pressure may be used together with catalyst composition, 4 0 4 0 0211501 112 Solvent Polamy and polymerlzfitlon to 1 Catalyst: A, AlEtzCl/B, AlEtClz/C, TiOLl/D, t-BuOH, pretreated trol the product molecular weight. As shown in Table I gg ggg g g C 1 hour for chlorobenzene diluent, the number average molecular 55 a Numbr average ii Weight ortotal olefin product,

4 No activity at 20 0. Only high molecular weight solid polymer was weight increased from 98.8 at atmospheric pressure to obtained upon increasing the temperature to 0. 147 at 500 p.s.1.a. 5 Pretreated at 20 C. for 30 minutes.

TABLE I Percent linear Mmoles 1 CH4 G. product] olefins in A/B/C/D Diluent Hours (p.s.1.a.) g. TiCh/hr. M 3 ClZ-Zl) 12 12/2/2 0511 01 1 15 45 98.8 67 12/12 2 2 O5H5Ol 1 55 95 100.5 70 12 12 2/2 Xylene 1 140 105 121.4 98 6/6/1/1 CGHsCL 1 105 147 112.0 97 3/3 05 05 CGH5C1. 2 250 74 121.3 99 12 12/2 2 Xylene 1 250 97 140.0 100 12 12 2/2 C6H5C1 0.5 500 126 147.0 100 1 Catalyst: A, AlEtzCl/B, AlEtCh/C, TiCh/D, t-BuOH. 2 Gaseous ethylene bubbled continuously through diluent at atmospheric pressure. 3 N umber average molecular weight of total olefin product.

EXAMPLE 3 Saturated, nonpolar solvents are completely ineffective The most effective alkyl aluminum halide Composition because they are inactive at the low temperatures needed has the formula AlR X where n is at least 1 but less to make liquid olefins. and y yield y plastics range than 2. This is shown in the following experiments which molecular weight (above about 20,000) at higher temwere carried out in the manner described in Example 2, 75 peratures (Run 14). Aromatic solvents are excellent (Run 16). The desired product is also obtainable when 50 volume percent of the aromatic is replaced by an aliphatic solvent under suitable conditions (Run 15), but the molecular weight would have been much higher it run at 150 p.s.i.a. The order of decreasing molecular weight with increasing solvent polarity for aliphatics is evident from Runs 14 to 17 and 18 to 19. Comparison of Runs 20, 21 and 22 shows that halogenated aliphatics produce the lowest molecular weight products. In Example 6 it is shown that the highest yields of detergent range olefins (C are obtained when the number average molecular weight is in the range between about 100 and 170. Therefore, the aromatics and halogenated aromatics are most preferred, although some halogenated aliphatic solvents could be used at considerably higher pressures.

EXAMPLE Reaction temperature must be controlled to a rather narrow, critical range in order to achieve high selectivities to C to C linear olefins. Experiments were performed as described in Example 4, except that polymerization temperature was varied at constant catalyst, diluent, and pressure. The results are summarized in Table IV below:

TABLE IV Mmoles 02H; 'Iemp., Run A/B/C/D 1 Diluent 2 (p.s.i.a.) 0. Mn

6/6/1/1 CaHaCL 151i) 0 137 6/6/1/1 OflHfi D 109 6/6/1/1 CaHaCl. 151) 30 100 4/4/2/0 Xylene" 121) 0 148 4/4/2/0 .do. 120 -20 111 1 Catalyst: A, AlEt G1/B, AlEtClz/C, TiCh/D, t-BuO El. 2 500 ml. diluent, 1 hour.

The average molecular weight increases with temperature for this catalyst system as shown in Table IV. It can also be seen from Table IV that the more polar solvents must be used at higher temperatures to achieve the desired molecular weight at any given ethylene pressure. However, there is an upper temperature limit, even with the halogenated solvents, at which the catalyst changes into the conventional Ziegler-type catalyst and produces mainly plastics range (high molecular weight) polyethylene. This upper limit is dependent upon solvent polarity and is in the range of about +15 to +25 C. A lower temperature limit also exists which is dependent upon solvent polarity and ethylene pressure. As shown in Table IV, the lower temperature limits for chlorobenzene and xylene are about 20 to C. at 150 p.s.i.a. It will be understood, however, that these temperatures could be slightly lower at higher ethylene pressures and still produce the desired average molecular weight linear olefins. Considering the interactions between catalyst composition, solvent polarity and ethylene pressure, the temperature range is about 30 to +10 C. for making detergent-range (C to C linear olefins.

EXAMPLE 6 The previously known branched, lubricating oil products which were made using similar catalysts, solvents and temperatures are characterized by a Poisson-type product distribution. The linear alpha olefins of this invention have been found to have a simple exponential distribution which corresponds to that which is commonly known as Florys most probable distribution (P. J. Flory, Principles of Polymer Chemistry, pages 334 to 339). Since the maximum theoretical yields of higher molecular weight olefins are lower for the simple exponential distribution than for a Poisson-type distribution, it is of critical importance to be able (1) to determine the theoretical limitations on selectivity which are imposed by the type of distribution, and (2) to find the critical conditions which produce the molecular weight average which yields maximum selectivity. For a simple exponential distribution, the optimum average molecular Weight does not usually coincide with the average molecular weight of the most detheoretical straight line. By relating the slope of each straight line to the number average molecular weight and then relating the latter to the selectivity to C to C olefins, it was found that there was a maximum selectivity of about 47 weight percent at a number average molecular weight of 134 for total product. In other words, selectivity decreases at both higher and lower average molecular weights. Therefore, in a process for making C to C olefins, depending upon whether the C to C or the C by-products are more valuable, the average molecular weight of the total product should thus be between about and 170, preferably to 145.

EXAMPLE 7 In other experiments similar to Examples 2 and 3, it has been found that (1) activity can be increased by pretreating the catalyst for a few minutes to several hours at temperatures below 25 C. (2) TiCl can be replaced by TiBr or TiCl OR where R=alkyl, aryl, aralkyl, cycloalkyl or benzoyl (3) TiCl, cannot be replaced by VCl, or FeCl because they produce high molecular weight polyethylene under the conditions described in Example 2 (4) replacing the AlEt Cl of Run 13 with AlBu Cl or AlMe Br gave substantially similar results, but phenyl aluminum chlorides were unsatisfactory and gave only high polymer, (5) t-butanol may be replaced by other alcohols, phenols, carboxylic acids and related compounds, and (6) Lewis bases such as ethers, tertiary amines or pyridine decrease catalyst activity.

EXAMPLE 8 A polymerization was carried out at 60 C. and 60 p.s.i.a. ethylene pressure using 6 mmoles AlEt Cl and 4 mmoles TiC1 in 250 ml. xylene. After 1 hour, product concentration was 11.2 weight percent, product linearity was 98.8 mole percent in the C to C fraction, and M was 75.9. The ethylene/product olefin mole ratio was 8.1.

This example illustrates that very low temperatures may be used and that low molecular weight products are obtained under these conditions.

It is to be understood that this invention is not limited to the specific examples which have been offered merely as illustrations and that modifications may be made without departing from the spirit of the invention as set forth in the claims.

What is claimed is:

1. The process for selectively preparing linear olefins having a number average molecular weight of about 70 to 300, which comprises polymerizing an ethylene-containing gas in the presence of a substantially soluble catalyst consisting of the reaction product of a transition metal halide selected from the group consisting of TiX TlXgOR', TiX OOCR', wherein X is selected from the group consisting of chlorine and bromine and R is selected from the group consisting of alkyl, aralkyl, and cycloalkyl, and an aluminum alkyl compound such that the ultimate formula of the aluminum alkyl compound is AlR X wherein R is selected from the group consisting of alkyl, aralkyl and cycloalkyl, X is selected from the group consisting of chlorine, bromine and iodine, and n is at least 1 but less than 2 in the presence of a diluent selected from the group consisting of aromatic hydrocarbons and halogenated hydrocarbons, at a temperature of less than 25 C. and an ethylene pressure above 50 p.s.i.a., wherein the mole ratio of ethylene to the reaction product is above 0.8 throughout the reaction and recovering the reaction product comprising at least 90 mole percent linear olefins in which the product olefin concentration is greater than 5 weight percent based on the diluent and reaction product.

2. A process as in claim 1 wherein said transition metal halide is TiCl 3. A process as in claim 1 wherein said ratio of ethylene to the reaction product is above about 2.0.

4. A process as in claim 1 wherein the diluent is an aromatic hydrocarbon.

5. A process as in claim 1 wherein the diluent is a halogenated aromatic hydrocarbon.

'6. A process for selectively preparing linear alpha olefins having a number average molecular weight of about 70 to 300 which comprises polymerizing an ethylone-containing gas in the presence of a soluble catalyst consisting of the reaction products of TiCl and an aluminum alkyl compound such that the ultimate formula of the aluminum alkyl compound is AlR X wherein R is ethyl and X is selected from the group consisting of bromine, chlorine and iodine and n is at least 1 but less than 2 in the presence of a diluent consisting of an aromatic hydrocarbon at a temperature of less than 25 C.

and an ethylene pressure above that 100 p.s.i.a., wherein the mole ratio of ethylene to the reaction product is above 0.8 throughout the reaction and recovering the reaction product comprising at least 90 mole percent linear alpha olefins in which the product olefin concentration is greater than 5 weight percent based on the diluent and reaction product.

7. A process as in claim 6 wherein said aluminum alkyl compound is diethyl aluminum chloride.

8. A process as in claim 6 wherein the diluent is xylene.

9. A process as in claim 6 wherein the pressure is above about 500 p.s.i.a.

10. A process as in claim 6 wherein the olefin concentration in the reaction product is greater than 10 weight percent based on the diluent and reaction product.

No references cited.

PAUL M. COUGHLAN, JR., Primary Examiner.

US. Cl. X.R. 26094.9 

